Scr catalyst device containing vanadium oxide and molecular sieve containing iron

ABSTRACT

The invention relates to a catalyst device for purifying exhaust gases containing nitrogen oxide by using selective catalytic reduction (SCR), the catalyst device comprising at least two catalytic layers, the first layer containing vanadium oxide and a mixed oxide comprising titanium oxide and silicon oxide and the second layer containing a molecular sieve containing iron, wherein the first layer is applied onto the second layer. The invention also relates to uses of the catalyst device and a method for purifying exhaust gases.

The invention relates to a catalyst device for purifying exhaust gasescontaining nitrogen oxide by using selective catalytic reduction (SCR),comprising at least two catalytic layers, the first layer containingvanadium oxide and the second layer containing a molecular sievecontaining iron, wherein the first layer is applied onto the secondlayer. The invention also relates to uses of the catalyst device and tomethods for purifying exhaust gases.

PRIOR ART

The method of selective catalytic reduction (SCR) is used in the priorart for reducing nitrogen oxides in exhaust gases, for example, fromcombustion plants, gas turbines, industrial plants or combustionengines. The chemical reaction is carried out with selective catalysts,hereinafter referred to as ‘SCR catalysts,’ which selectively removenitrogen oxides, especially NO and NO₂, by reduction. In contrast,undesirable side reactions are suppressed. In the reaction, a reductantcontaining nitrogen is fed in, usually ammonia (NH₃) or a precursorcompound, such as urea, which is added to the exhaust gas. The reactionis a comproportionation. Essentially water and elemental nitrogen areobtained as reaction products. SCR catalysts often contain metal oxides,such as oxides of vanadium, titanium, tungsten, zirconium orcombinations thereof. As SCR catalysts, molecular sieves are also oftenused, in particular zeolites, which are exchanged with catalyticallyactive metals.

An important application of SCR is the removal of nitrogen oxides fromexhaust gases from combustion engines which are predominantly operatedwith a lean air/fuel ratio. Such combustion engines are diesel enginesand direct-injection gasoline engines. These are collectively referredto as ‘lean-burn engines.’ In addition to the harmful gases carbonmonoxide CO, hydrocarbons HO and nitrogen oxides NOx, the exhaust gasfrom lean-burn engines contains a relatively high oxygen content of upto 15 vol %. Carbon monoxide and hydrocarbons can easily be renderedharmless by oxidation. The reduction of nitrogen oxides to nitrogen ismuch more difficult due to the high oxygen content.

Since combustion engines in motor vehicles are operated transiently, theSCR catalyst must guarantee the highest possible nitrogen oxideconversions with good selectivity even under strongly fluctuatingoperating conditions. A complete and selective nitrogen oxide conversionat low temperatures must be ensured, as must the selective and completeconversion of high nitrogen oxide quantities in very hot exhaust gas,for example during full load driving. In addition, the stronglyfluctuating operating conditions cause difficulties with the exactdosing of the ammonia, which should ideally take place in astoichiometric ratio to the nitrogen oxides to be reduced. This placeshigh demands on the SCR catalyst, i.e. on its ability to reduce nitrogenoxides to nitrogen with high conversion and selectivity rates in a widetemperature window with highly variable catalyst loads and a fluctuatingsupply of reductant.

EP 0 385 164 B1 describes so-called ‘full catalysts’ for the selectivereduction of nitrogen oxides with ammonia, which, in addition totitanium oxide and at least one oxide of tungsten, silicon, boron,aluminum, phosphorus, zirconium, barium, yttrium, lanthanum and cerium,contain an additional component selected from the group of oxides ofvanadium, niobium, molybdenum, iron and copper.

U.S. Pat. No. 4,961,917 relates to catalyst formulations for reducingnitrogen oxides with ammonia, which, in addition to zeolites with asilica:alumina ratio of at least 10 and a pore structure which is linkedin all spatial directions by pores having an average kinetic porediameter of at least 7 angstroms, contain iron and/or copper aspromoters.

However, the catalyst devices described in the above documents need tobe improved, because good nitrogen oxide conversion rates can only beachieved at relatively high temperatures of above approximately 350° C.or above approximately 450° C. As a rule, optimum conversion only takesplace within a relatively narrow temperature range. Such an optimumconversion is typical for SCR catalysts and is determined by themechanism of action.

The reaction of nitrogen oxides on SCR catalysts with ammonia, which canbe formed from a precursor compound such as urea, is carried outaccording to the following reaction equations:

4NO+4NH₃+O₂→4N₂+6H₂  (1)

NO+NO₂+2NH₃→2N₂+3H₂O  (2)

6NO₂+8NH₃→7N₂+12H₂O  (3)

It is advantageous to increase the proportion of NO₂ and, in particular,to adjust an NO₂:NO ratio of approximately 1:1. Under these conditions,significantly higher conversion rates can already be achieved at lowtemperatures below 200° C. due to the significantly faster reaction (2)(‘rapid SCR reaction’) as compared to reaction (1) (‘standard SCRreaction’).

However, the nitrogen oxides NOx contained in the exhaust gas fromlean-burn engines consist predominantly of NO and have only smallproportions of NO₂. In the prior art, an upstream oxidation catalyst,for example, platinum supported on alumina, is therefore used for theoxidation of NO to NOx.

A further problem with the removal of nitrogen oxides in the exhaust gasof lean-burn engines with SCR catalysts is that the ammonia is oxidizedto low-valent nitrogen oxides, especially nitrous oxide (N₂O), due tothe high oxygen content. This removes the reductant required for the SCRreaction from the process on the one hand, and the nitrous oxide escapesas an undesired secondary emission on the other hand.

In order to solve the described goal conflicts and to be able to ensurethat nitrogen oxides are removed at all operating temperatures occurringduring driving operation, which often lie between 180° C. and 600° C.,combinations of various SCR catalysts which are to combine advantageousproperties are proposed in the prior art.

US 2012/0275977 A1 relates to SCR catalysts in the form of molecularsieves. These are zeolites containing iron or copper. In order to removenitrogen oxides as comprehensively as possible, various molecular sieveswith different functionalities are preferably combined.

US 2012/0058034 A1 proposes combining zeolites with a further SCRcatalyst based on oxides of tungsten, vanadium, cerium, lanthanum andzirconium. The zeolites are mixed with the metal oxides and a suitablesubstrate is coated therewith, whereby a single catalyst layer havingboth functionalities is obtained.

In the prior art, vanadium-based SCR catalysts were also combined withiron-exchanged zeolites. For example, WO 2014/027207 A1 discloses SCRcatalysts containing, as a first catalytic component, an iron-exchangedmolecular sieve and, as a second component, a vanadium oxide coated on ametal oxide selected from aluminum, titanium, zirconium, cerium orsilicon. The various catalysts are mixed and a single catalytic coatingis produced on a suitable substrate. However, the efficiency of such acatalyst in the temperature range below 450° C. and especially below350° C. is still in need of improvement.

WO 2009/103549 discloses combinations of zeolites and vanadium oxide incombination with further metal oxides. In order to improve catalystefficiency, it is proposed that the catalyst be divided into zones. Azone with the zeolite, which serves as an NH₃ storage component, islocated on the exhaust gas inlet side. A zone with the SCR-activecomponent, which contains the vanadium—based SCR catalyst, then adjoinson the outlet side. The zeolite has only one storage function, while thefollowing component catalyzes the SCR reaction with vanadium oxide.

WO 2008/006427 A1 relates to combinations of iron-exchanged zeoliteswith copper-exchanged zeolites. It specifically proposes coating aceramic substrate first with the copper-exchanged zeolite, and forming acoating with the iron-exchanged zeolite over it. In these ways, thedifferent activities of the layers within different temperature rangesare to be combined in an advantageous manner.

WO 2008/089957 A1 proposes to equip a ceramic substrate with a lowercoating containing vanadium oxide and an upper coating containingiron-exchanged zeolites. The upper coating with the iron-exchangedzeolite is intended to prevent nitrous oxide from being formed at highoperating temperatures.

EP 2 992 956 A1 describes an SCR catalyst having a ‘dual-layerstructure,’ wherein a layer containing V₂O₅/TiO₂ lies upon a layercomprising a metal-exchanged zeolite.

DE 10 2014 002 751 A1 also discloses an SCR catalyst comprising twolayers located upon a catalyst honeycomb body. While the lower layer cancomprise zeolites exchanged with iron or copper, the upper layercomprises vanadium pentoxide and titanium dioxide.

SCR catalysts comprising vanadium-based formulations and Cu or Fezeolites are also disclosed in WO 2016/011366 A1, DE 10 2006 031 661 A1as well as in Ind.Eng.Chem.Res. 2008, 47, 8588-8593.

The SCR catalysts described are however still in need of improvementwith regard to their efficiency. There is a continuous need forcatalysts that are highly efficient under various applicationconditions. In particular, there is a need for catalysts that aresuitable for the purification of both NO-rich and NO₂-rich exhaust gasesand that operate efficiently over the entire temperature range of commonapplications, that is, at low and medium temperatures as well.

Another problem with conventional catalysts is that nitrous oxide isformed in conventional applications involving combustion engines. Thisproblem is particularly evident in the middle and low temperature rangebelow about 450° C. or below about 350° C. Exhaust gases from combustionengines often have such temperatures during normal operation, which canlead to the undesirable formation and release of nitrous oxide.

J.Phys.Chem. C2009, 113, 2, 1177-21184 reports that the conversion ofnitrogen monoxide (NO) with ammonia on V₂O₅—WO₃/TiO₂ SCR catalysts canbe improved by adding cerium oxide to the SCR catalysts mentioned.However, the measurements carried out involved SCR catalysts whichcontained only 0.1 wt % vanadium and are therefore irrelevant inpractice. The same applies with regard to the data reported in Progressin Natural Science Materials International, 25 (2015), 342-352. Thedocuments do not contain any data concerning the conversion of nitrogendioxide (NO₂).

J.Fuel.Chem.Technol., 2008, 36(5), 616-620 also includes data on theinfluence of the cerium oxide content on V₂O₅—CeO₂/TiO₂ SCR catalysts inthe conversion of nitrogen monoxide (NO) with ammonia. Positive effectsof cerium oxide are accordingly observed only with contents of 20 wt %and above. The document does not contain any data concerning theconversion of nitrogen dioxide (NO₂).

It is known that NOx conversion with ammonia in the presence of V/TIO₂SCR catalysts depends very strongly on the NO₂/NOx molar ratio; see, forexample, Environmental Engineering Science, Vol. 27, 10, 2010, 845-852,in particular FIG. 2. Thus, the results of the conversion of NO cannotbe used to predict results in the conversion of NO₂ or of NOx with ahigh NO₂ proportion.

Studies conducted by the inventors of the present application show thatthe conversion of nitrogen oxides with ammonia at low temperatures onSCR catalysts containing vanadium and cerium depends in particular onthe composition of the nitrogen oxide. In the case that the nitrogenoxide consists only of nitrogen monoxide (NO), the conversion decreasesas the cerium oxide content increases. However, this changes as thecontent of nitrogen dioxide (NO₂) increases. Thus, for example, with anitrogen dioxide content of 75%, the conversion increases as the ceriumoxide proportion increases; see FIGS. 6 and 7.

Object of the Invention

The invention is based upon the object of providing catalysts, methodsand uses that overcome the disadvantages described above. In particular,SCR catalysts are to be provided which enable an efficient removal ofnitrogen oxides over a wide temperature range, and thus also at low andmedium temperatures. Here, nitrogen oxides NOx, in particular NO andNO₂, should be efficiently removed while at the same time the formationof nitrous oxide N₂O is to be prevented. The catalysts should have ahigh efficiency, especially in the temperature range of 180° C. to 600°C., which is regularly of importance in combustion engines.

The catalysts should be suitable for purifying exhaust gases having arelatively high proportion of NO₂, in particular when the NO₂:NO ratiois ≥1:1. Here, the catalysts should be efficient even at lowtemperatures, where catalysts of the prior art are often less efficient,for example, below 450° C. or below 350° C. The catalysts should also besuitable for purifying exhaust gases having a relatively high proportionof NO.

In particular, catalysts are to be provided that combine the followingadvantageous properties;

-   -   a high efficiency with exhaust gases rich in NO₂ in the        temperature range from about 180° C. to 600° C., and in        particular at low temperatures,    -   a high efficiency with exhaust gases rich in NO, and    -   the prevention of the formation of nitrous oxide.

The catalysts should preferably be effective both immediately aftertheir production and also after a prolonged period of use and aging.

DISCLOSURE OF THE INVENTION

Surprisingly, the object underlying the invention is achieved bycatalyst devices, uses and methods according to the claims.

The object of the invention is a catalyst device for purifying exhaustgases containing nitrogen oxide by selective catalytic reduction (SCR),said device comprising at least two catalytic layers, wherein the firstlayer contains vanadium oxide and a mixed oxide comprising titaniumoxide and silicon oxide and the second layer contains a molecular sievecontaining iron, the first layer being applied onto the second layer.

The catalyst device is used for reducing nitrogen oxides (‘NOx’) inexhaust gases by the method of ‘selective catalytic reduction’ (SCR).The exhaust gases can, for example, come from combustion engines,combustion plants, gas turbines or industrial plants. During the SCR,nitrogen oxides, especially NO and NO₂, are selectively reduced. Thereaction takes place in the presence of a reductant containing nitrogen,typically ammonia (NH₃) or a precursor compound thereof, such as urea.The reductant containing nitrogen is usually added to the exhaust gas.

The catalyst includes at least two catalytic layers, wherein a first,upper catalytic layer is disposed on the second, lower catalytic layer.‘Catalytic’ here means that each of the layers has catalytic activityduring the SCR. It is particularly preferred that the first, upper layerbe in direct contact with the exhaust gases. This means that the firstlayer is the outermost layer over which no further layer is applied. Itis however also possible according to the invention for at least onefurther functional layer, which serves, for example, to pre-treat theexhaust gases, to be present above the first layer. This pre-treatmentcan be, for example, a catalytic pre-treatment.

Within the context of this application, the term ‘metal oxide’ generallyrefers to oxides of the metal. Thus, the term does not refer solely tothe metal monoxide with a stoichiometric ratio of 1:1. The term ‘metaloxide’ in this case designates both specific oxides and also mixtures ofvarious oxides of the metal.

Within the context of this application, the term ‘mixed oxide’ excludesphysical mixtures of two or more metal oxides. Rather, it stands for‘solid solutions’ with a uniform crystal lattice, in which theindividual metal oxides can no longer be distinguished or it stands formetal oxide agglomerates that do not have a uniform crystal lattice andin which phases of the individual metal oxides can be distinguished.

The first, upper layer contains vanadium oxide, which is preferablypresent as vanadium pentoxide V₂O₅. In this respect, it is not ruled outthat a portion of the vanadium has a different oxidation state and ispresent in a different form. The vanadium oxide is preferably thecrucial catalytically active component of the first layer which islargely responsible for the reaction. Hence, the first catalytic layeris hereinafter also referred to for short as the ‘vanadium catalyst.’

The first, upper layer also contains a mixed oxide comprising titaniumoxide and silicon oxide.

In a preferred embodiment, the first layer contains at least one furthercomponent selected from oxides of tungsten and aluminum. The first layerparticularly preferably contains oxides of vanadium, silicon, tungstenand titanium, preferably in the form of V₂O₅, SiO₂, WO₃ and TiO₂.

In this case, the metal oxides can have catalytic activity during theSCR or contribute to catalytic activity. According to the invention,vanadium oxide and tungsten oxide, for example, have catalytic activity.

The metal oxides can also have little or no catalytic activity and canserve, for example, as substrate material. Such non-catalytic componentsserve, for example, to enlarge the inner surface area of the catalystand/or to create a porous structure. Titanium oxide, for example,preferably serves as substrate material. It may contain proportions ofother non-reactive or only slightly reactive metal oxides, such assilicon dioxide or aluminum trioxide. The substrate material isgenerally present in excess, wherein the catalytic component isgenerally applied to the surface of the inert component.

In a preferred embodiment, the main component of the first, upper layeris titanium dioxide making up, for example, more than 50 wt %, more than80 wt % or more than 90 wt % of the layer. For example, a catalyst layerbased on oxides of vanadium, silicon, titanium and tungsten essentiallycontains TiO₂ in the anatase modification. TiO₂ can be stabilized by WO₃in order to achieve an improvement in thermal durability. In this case,the proportion of WO₃ is typically from 5 to 15 wt %, for example, from7 to 13 wt %.

An advantage of the catalytic component based on vanadium oxide is itshigh activity during the SCR at low temperatures. According to thepresent invention, the low-temperature activity of the vanadium-basedcatalysts is advantageously combined with the specific activity of themolecular sieves containing iron so as to provide a catalyst havingexcellent cold-start properties.

In a preferred embodiment, the first layer additionally contains ceriumoxide. Surprisingly, it has been found that SCR efficiency can beimproved significantly by combinations of vanadium oxide with ceriumoxide. The effect is particularly pronounced with a longer operatingtime of the catalyst, associated with aging of the catalyst. It has thusbeen found that after aging of the catalyst, both the removal ofnitrogen oxides and the prevention of the formation of N₂O isparticularly effective if the vanadium catalyst in the first layeradditionally contains cerium oxide. In general, the advantageous effectof cerium oxide is manifested above all in the low temperature range, inparticular below 400° C., and especially in the range from 180 to 400°C. This is of particular advantage since it is at low temperatures thatthe optimal removal of nitrogen oxides and the prevention of theformation of nitrous oxide are particularly problematic. These effectsare particularly pronounced in exhaust gas rich in NO₂, that is, whenNO₂:NOx>0.5.

The catalyst preferably comprises from 0.5 to 10 wt %, in particularfrom 1 to 5 wt %, vanadium oxide, calculated as V₂O₅ and based on theweight of the first layer. The catalyst preferably comprises from 0.5 to15 wt %, in particular from 1 to 7 wt %, silicon dioxide, calculated asSiO₂ and based on the weight of the first layer. The catalyst preferablycomprises from 1 to 17 wt %, in particular from 2 to 10 wt %, tungstenoxide, calculated as WO₃ and based on the weight of the first layer. Thecatalyst preferably comprises from 0.2 to 10 wt %, in particular from0.5 to 5 wt % or from 0.5 to 3 wt %, cerium oxide, calculated as CeO₂and based on the weight of the first layer. The statement ‘calculatedas’ takes into account that in this technical field, elemental analysisgenerally determines the quantities of metals.

In a preferred embodiment, the first layer preferably contains orconsists of the following oxides of metals:

-   -   (a) from 0.5 to 10 wt % vanadium oxide, calculated as V₂O₅,    -   (b) from 0 to 17 wt % tungsten oxide, calculated as WO₃,    -   (c) from 0 to 10 wt % cerium oxide, calculated as CeO₂,    -   (d) from 25 to 98 wt % titanium oxide, calculated as TiO₂,    -   (e) from 0.5 to 15 wt % silicon oxide, calculated as SiO₂,    -   (f) from 0 to 15 wt % aluminum oxide, calculated as Al₂O₃        in each case based on the weight of the first layer.

The first layer particularly preferably contains vanadium dioxide,cerium oxide, titanium dioxide and silicon dioxide but not tungstenoxide.

The first layer also preferably contains 0.5 to 10 wt % vanadium oxide;2 to 17 wt. % tungsten oxide; 0 to 7 wt % cerium oxide, as well as 25 to98 wt % titanium dioxide, based on the weight of the first layer.

Likewise, the first layer particularly preferably contains vanadiumoxide, tungsten oxide, cerium oxide, titanium dioxide and silicondioxide.

In this case, the first layer preferably has the following composition:

-   -   (a) from 1 to 5 wt % vanadium oxide, calculated as V₂O₅,    -   (b) from 1 to 15 wt % tungsten oxide, calculated as WO₃,    -   (c) from 0.2 to 5 wt % cerium oxide, calculated as CeO₂,    -   (d) from 73 to 98 wt % titanium dioxide, and    -   (e) from 0.5 to 25 wt % silicon dioxide,        wherein the sum of the proportions of cerium oxide+tungsten        oxide is less than 17 wt %, in each case based on the weight of        the first layer.

The catalyst includes a second catalytic layer underlying the firstlayer with the vanadium catalyst. This second layer contains a molecularsieve containing iron.

The term ‘molecular sieve’ refers to natural and synthetic compounds, inparticular zeolites, which have a strong adsorptive capacity for gases,vapors and dissolved substances of specific molecular sizes. By suitablyselecting the molecular sieve, it is possible to separate molecules ofdifferent sizes. Besides zeolites, aluminum phosphates, in particularsilicon aluminum phosphates, are, for example, also known. Molecularsieves generally have uniform pore diameters which are in the order ofmagnitude of the diameters of molecules and have a large inner surfacearea (600-700 m²/g).

In a particularly preferred embodiment, the molecular sieve is azeolite. The term ‘zeolite’ is generally understood according to thedefinition of the International Mineralogical Association (D. S. Coombset al., Can. Mineralogist, 35, 1997, 1571) to mean a crystallinesubstance from the group of aluminum silicates that has athree-dimensional network structure of the general formulaM^(n+)[(AlO₂)X(SiO₂)Y]xH₂O. The basic structure is formed from SiO₄/AlO₄tetrahedra, which are linked by common oxygen atoms to form a regularthree-dimensional network. The zeolite structure contains cavities andchannels that are characteristic of each zeolite. The zeolites areclassified into different structures according to their topology. Thezeolite framework contains open cavities in the form of channels andcages that are normally occupied by water molecules and specialframework cations that can be exchanged.

The inlets to the cavities are formed by 8, 10 or 12 ‘rings’(narrow-pored, medium-pored and wide-pored zeolites). In a preferredembodiment, the zeolite has a structure in the second, lower layer whosemaximum ring size is defined by more than 8 tetrahedra.

According to the invention, zeolites with the topologies AEL, AFI, AFO,AFR, ATO, BEA, GME, HEU, MFI, MWW, EUO, FAU, FER, LTL, MAZ, MOR, MEL,MTW, OFF and TON are preferred. Zeolites of the topologies FAU, MOR,BEA, MFI and MEL are particularly preferred.

In the context of the present invention, preference is given to using azeolite, in particular any 10-ring and 12-ring zeolite, which has aSiO₂/Al₂O₃ molar ratio (SAR ratio) of 5:1 to 150:1. The SiO₂/Al₂O₃ ratiopreferred according to the invention lies within the range from 5:1 to50:1 and particularly preferably within the range from 10:1 to 30:1.

The molecular sieve in the second layer contains iron and is preferablyan iron-containing zeolite. It has been found that iron-containingzeolites in combination with the first layer containing vanadium oxidecatalyze a particularly efficient SCR in the layer arrangement accordingto the invention. Preference is given to using a zeolite which isexchanged with iron ions (‘iron-exchanged zeolite’) or in which at leasta portion of the aluminum atoms of the aluminosilicate framework isisomorphously substituted with iron, thus forming a ferrosilicateframework.

The zeolite is particularly preferably exchanged with iron. The zeoliteis preferably one of the BEA type. Very particular preference is givento an iron-exchanged zeolite of the BEA type with an SAR of 5:1 to 50:1.Methods for producing iron-containing zeolites, for example via solid orliquid phase exchange, are known to the person skilled in the art. Theproportion of iron in the iron-containing zeolite is, for example, up to10% or up to 15%, calculated as Fe₂O₃ and based on the total amount ofthe iron-containing zeolite, Zeolites containing iron and iron-exchangedzeolites preferred according to the invention are described, forexample, in US 2012/0275977 A1.

In a preferred embodiment, the second layer contains at least twodifferent iron-containing zeolites. It is advantageous in this case thatvarious desired properties can be combined. For example, aniron-containing zeolite that is active at low temperatures can becombined with an iron-containing zeolite that is active at highertemperatures.

Instead of an iron-containing zeolite, the second layer can also containa ferrosilicate or ferrosilicates.

The second, lower layer can contain further components in addition tothe molecular sieve containing iron, in particular catalyticallyinactive components, such as binders. For example, catalyticallyinactive or only slightly catalytically active metal oxides, such asSiO₂, Al₂O₃ and ZrO₂, are, for example, suitable as binders. Theproportion of such binders in the second layer is, for example, up to15%.

The thickness of the first and second layer and the amount of catalystsin the first and second layers are adjusted to each other so as toobtain a desired removal of nitrogen oxides.

In a preferred embodiment, the catalyst device additionally comprises asubstrate in addition to the first and second coating. The substrate isa device onto which the catalytic coatings are applied. The substrate isnot catalytically active here, i.e. it is inert as regards the reaction.The substrate may be a metallic or ceramic substrate. The substrate mayhave a honeycomb structure of parallel exhaust gas flow channels or be afoam. In a preferred embodiment, the substrate is a monolith. Monolithsare one-piece ceramic substrates which are used in particular in theautomotive industry and have parallel channels which run from the inletside to the outlet side and through which the exhaust gases flow. Thisstructure is also referred to as a ‘honeycomb.’ Alternatively, thesubstrate can be a filter, in particular a wall-flow filter, in whichthe exhaust gases flow on the inlet side into channels closed on theoutlet side, flow through the channel walls and then leave the substratethrough channels closed on the inlet side and open on the outlet side.

In a further embodiment, the second, lower layer simultaneously servesas a substrate. This is possible in particular if the second, lowercatalytic layer is provided as an extrudate. In this case, the second,lower layer itself forms a substrate device onto which the first, upperlayer is applied. Such a substrate device is obtainable, for example,when the iron-containing zeolite is incorporated into the walls of theexhaust gas channels. This embodiment has the advantage that noadditional inert substrate is required so that the interior of thecatalyst device can be given a particularly compact design.

In a further preferred embodiment, the second layer is applied directlyonto the substrate. Alternatively, at least one further functionallayer, for example, a further catalytic layer having different catalystcompounds and thereby introducing a further activity, can also bepresent between the substrate and the second layer.

The entire interior of the catalyst device according to the invention ispreferably coated. This means that all regions which the exhaust gasescontact are coated. It is preferable here that the entire interior isfully coated with the first and second layer. In this embodiment, aparticularly efficient conversion of nitrogen oxides is obtained sincethe entire inner surface area of the device is used catalytically.

In general, it is highly preferred for the exhaust gases to first comeinto contact in the flow direction with the first, upper layer whichcomprises the vanadium catalyst. Without being bound by any theory, itis assumed that an exhaust gas fraction, which was pre-treated with thevanadium catalyst, then advantageously reacts with the iron-containingzeolite so that a particularly efficient depletion of nitrogen oxides isachieved while simultaneously preventing the formation of nitrous oxide.In particular, it has been found that the arrangement of the catalystsin this order leads to a particularly efficient purification of NOx,even at relatively low temperatures, and to the prevention of theformation of nitrous oxide, particularly in the case of high levels ofNO₂ in the NOx.

In a preferred embodiment, the second layer is applied completely to thesubstrate. In this case, the first layer may be present on the secondlayer completely or only partially (in one or more zones).

In a preferred embodiment, the first layer is applied completely to thesecond layer. This means that there is no region on the inner surface ofthe catalyst device in which the lower, second layer is in directcontact with the exhaust gases. In this case, it is advantageous thatonly exhaust gases that have been pre-treated in the first, upper layerreach the lower, second layer.

In a further preferred embodiment, the first layer is applied onto thesecond layer in certain regions. In this embodiment, there are regionsin which the lower, second layer comes into direct contact with theexhaust gases. In this case, it is highly preferred that the exhaustgases first come into contact with the first, upper layer. Thus, it isespecially preferred that a region which has a first, upper layer isfirst in the flow direction. In this embodiment, it is also ensured thatthe exhaust gases first come into contact with the upper layercontaining the vanadium catalyst and are thereby pre-treated before theyreach the second layer.

In a preferred embodiment, the exhaust gases as they leave the catalystdevice lastly come into contact with the first, upper layer. A reactionwith the vanadium oxide thus takes place last. In this case, the second,lower layer is preferably present beneath the first, upper layer at theoutlet of the catalyst device. In such an embodiment of the device, theSCR is particularly efficient.

For the reasons stated, it is altogether particularly preferred for theinterior of the catalyst device to be completely equipped with thesecond, lower layer, on which the first, upper layer is completelypresent.

In a further preferred embodiment, the first layer or the second layerconsists of two or more superimposed sub-layers. The sub-layers candiffer, for example, with regard to their physical properties, such asdensity or porosity, or their chemical properties, such as thecomposition of the individual components. For example, the first, upperlayer can consist of an upper sub-layer which contains vanadium oxideand a lower sub-layer which contains vanadium oxide and additionallycerium oxide. The lower, second layer can, for example, consist of afirst and a second sub-layer that contain iron-containing zeolites withvarious activities. In these embodiments, it is advantageous that by asuitable selection and by combinations of different catalysts of thesame type, their properties can be combined in a targeted manner inorder, for example, to obtain a reactivity within a wide temperaturerange.

In a further embodiment, the catalyst device has different regions(zones) which follow one another in the exhaust-gas flow direction. Inthis case, different catalysts of the first and/or the second layer canbe combined in different zones in order to obtain advantageousproperties of the catalyst device. It is thus conceivable, for example,for a zone with a first and second catalyst to be present on the inletside, said zone being particularly efficient at relatively hightemperatures, while toward the outlet side there is a zone which has anactivity optimum at a lower temperature. The catalyst device may have aplurality of successive zones, for example 2, 3, 4 or 5 zones.

In a preferred embodiment, the catalyst device has no further layersbeyond the first and the second layer, in particular no furthercatalytic layers, and above all no further layers containing vanadiumoxide or iron-containing zeolites.

The catalyst device preferably does not contain any noble metal. Inparticular, the first and second layers do not contain any noble metals,such as platinum, gold, palladium and/or silver. According to theinvention, a catalyst device having a high efficiency is providedwithout requiring the use of noble metals that are expensive and notavailable in large quantities.

The SCR catalyst is applied using methods known in the prior art, forexample, by applying coating suspensions (so-called ‘wash coats’), bycoating in an immersion bath or by spray coating. The lower layer mayalso be an extrudate. Application of the coatings with wash coats isparticularly preferred. As is generally customary, wash coats refer tocoating suspensions in which the solids or precursor compounds aresuspended and/or dissolved in order to produce the catalytic layers.Such wash coats are provided in a very homogeneous form with finelydistributed constituents so that the substrates can be coated asuniformly as possible. After application of the wash coats, the usualpost-treatment steps follow, such as drying, calcining and tempering.

In a preferred embodiment, the ratio of the weight (per catalyst volume)of the first to the second layer in the catalyst device is greater than0.2, in particular is between 0.2 and 15, and particularly preferably isbetween 1 and 6.

The total amount of coating is selected such that the device as a wholeis utilized as efficiently as possible. In the case of a flow-throughsubstrate, for example, the total amount of coatings (solids content)per substrate volume (total volume of the catalyst device) may bebetween 100 and 600 g/l, in particular between 100 and 500 g/l.Preferably, the second, lower layer is used in a quantity of 50 to 200g/l, in particular between 50 and 150 WI, particularly preferably ofapproximately 100 WI. The first, upper layer is preferably used in anamount of 100 to 400 g/l, in particular between 200 and 350 g/l,particularly preferably about 280 g/l. In the case of a filtersubstrate, substantially less wash coat is generally used, for example,in a total amount of 10 to 150 g/l.

The invention also relates to the use of a catalyst device according tothe invention for purifying exhaust gases containing nitrogen oxide byselective catalytic reduction (SCR).

Likewise, the present invention also relates to a method for removingnitrogen oxides from the exhaust gas of combustion engines operated witha lean air/fuel ratio, said method being characterized in that theexhaust gas is passed through a catalyst device according to theinvention.

The method according to the invention is particularly advantageous whenthe NO₂ proportion in the nitrogen oxide exceeds 50% (NO₂/NO>0.5), i.e.is, for example, 75%.

The exhaust gases are preferably those from combustion plants. Thecombustion plants can be mobile or stationary. For the purposes of thisinvention, mobile combustion devices are, for example, the combustionengines of motor vehicles, in particular diesel engines. Stationarycombustion devices are usually power plants, combustion plants, orheating systems in private households.

The exhaust gases preferably originate from lean-burn engines, that isto say, combustion engines operated predominantly with a lean air/fuelratio. Lean-burn engines are in particular diesel engines anddirect-injection gasoline engines.

Depending on various influencing factors (such as engine calibration,operating state, type and design of upstream catalysts), the NO₂proportion in the NOx may exceed 50%. According to the invention, it hasbeen found that the catalyst device particularly efficiently catalyzesthe SCR of exhaust gases with a high NO₂ content (NO₂/NOx>0.5), namelyeven in the problematic medium to low temperature range below about 450°C., in particular below 350° C. In particular, it has been found thatwith such exhaust gases, an efficient removal of the nitrogen oxides isachieved with a simultaneous prevention of the formation of nitrousoxide. These results were surprising since it was known in the prior artthat vanadium catalysts are relatively inefficient in the SCR withexhaust gases rich in NO₂, especially at low temperatures, while themore efficient iron-zeolite catalysts produce a high proportion of N₂O.

In a preferred embodiment, the exhaust gases originate from an upstreamoxidation catalyst. Such upstream oxidation catalysts are used in theprior art among other things in order to increase the proportion of NO₂in the case of exhaust gases from lean-burn engines, in particulardiesel engines.

When introduced into the catalyst device, the exhaust gases preferablyhave a relatively high oxygen content which is, for example, at least 5vol %, at least 10 vol %, or at least 15 vol %. Exhaust gases fromlean-burn engines regularly have such high oxygen contents. Theoxidizing agent, oxygen, makes the reductive removal of nitrogen oxidesby means of SCR more difficult. Surprisingly, it has been found that thecatalyst devices according to the invention also efficiently removenitrogen oxides from exhaust gases with a high oxygen content and at thesame time prevent the formation of nitrous oxide.

Preferably, during the SCR reaction of exhaust gases with the catalystdevice according to the invention, more than 90%, preferably more than95%, of NOx and/or NO₂ are removed.

According to the invention, it is advantageous that an efficientpurification of exhaust gases by SCR can also take place at relativelylow temperatures, wherein it is precisely at low temperatures that theformation of nitrous oxide can be prevented. The use of the catalystdevice is particularly advantageous at temperatures in the range below450° C., in particular from 180 to 450° C., and particularly preferablybetween 200 and 350° C.

In a preferred embodiment, it is used for preventing the formation ofnitrous oxide (N₂O), in particular in the purification of exhaust gasesrich in NO₂ and in particular at temperatures below 450° C. or below350° C. According to the invention, it has been found that an efficientdepletion of nitrogen oxides can take place, while at the same time theformation of nitrous oxide is prevented or relatively little nitrousoxide is produced. According to the prior art, relatively high amountsof nitrous oxide form during the SCR reaction with vanadium catalystsand iron-containing zeolites, in particular in the purification ofexhaust gases rich in NO₂ at low or even medium temperatures. It wastherefore surprising that the arrangement according to the invention ofthe first and second layer results in an efficient SCR and at the sametime only relatively small quantities of nitrous oxide are produced.Preferably, the concentration of nitrous oxide after the SCR with thecatalyst device according to the invention is not higher than 50 ppm, 20ppm or 10 ppm. In particular, such concentrations are not to be exceededat temperatures ranging from 180° C. to 450° C., in particular from 200°C. to 350° C.

The invention also relates to a method for purifying exhaust gases,comprising the steps:

-   -   (i) Providing a catalyst device according to the invention,    -   (ii) Introducing exhaust gases containing nitrogen oxides into        the catalyst device,    -   (iii) Introducing a reductant containing nitrogen into the        catalyst device, and    -   (iv) Reducing nitrogen oxides in the catalyst device by        selective catalytic reduction (SCR).

The method according to the invention is particularly advantageous whenthe NO₂ proportion in the nitrogen oxide exceeds 50% (NO₂/NOx>0.5), i.e.is, for example, 75%.

The exhaust gases introduced in step (ii) preferably come from lean-burnengines, in particular from an oxidation catalyst downstream of theengine. In the method, the catalyst device according to the inventioncan be combined in series or in parallel with further devices forpurifying exhaust gases, such as further catalysts or filters.

During the SCR reaction, a reductant containing nitrogen, preferablyammonia (NH₃) or a precursor compound thereof, such as urea, is added.The reductant containing nitrogen is preferably added to the exhaust gasbefore it enters the catalyst device, but it can also be introducedseparately into the catalyst device.

The catalyst device according to the invention achieves the objectunderlying the invention. A catalyst device for purifying exhaust gasesby SCR is provided, which efficiently removes nitrogen oxides whilepreventing the formation of nitrous oxide. The device is suitable forpurifying exhaust gases over a wide temperature range. It is suitablefor purifying exhaust gases rich in NO₂ which arise in the operation ofdiesel engines, for example in conjunction with an oxidation catalyst.Even after aging, the catalyst device exhibits a high level of catalyticactivity and prevents or minimizes the formation of nitrous oxide. Theeffect according to the invention can even be improved by adding ceriumoxide to the vanadium catalyst, wherein among other things a furtherreduction of nitrous oxide, in particular at low temperature, can beachieved. Due to the high efficiency during the SCR under variousconditions of use, even at low temperature and with both low and highNO₂ contents, the catalyst devices are highly suitable for applicationsin the automotive field.

FIGS. 1 to 5 show in graph form the results of the SCR reactionaccording to Exemplary Embodiment 3 with model exhaust gases withcatalyst devices according to the invention and comparative devices,which were produced according to Example 2. In all of the figures,measured values are given for different temperatures of the modelexhaust gases. Figures a and b each show the proportion of NOx removedfrom the model exhaust gas by the catalyst device. Figures c in eachcase indicate the concentration of N₂O that was measured after thecatalyst device.

FIGS. 6 and 7 show the dependence of the conversion on the respective NOand NO₂ content of the exhaust gas.

EXEMPLARY EMBODIMENTS

Preliminary Tests

FIGS. 1 and 2 show the dependence of the conversion of nitrogen monoxide(see FIG. 1) or of nitrogen dioxide (NO₂/NOX=75%) (see FIG. 2) on thecerium content of the SCR catalyst.

In FIGS. 1 and 2:

Reference=SCR catalyst consisting of 3% V₂O₅, 4.3% WO and the remainderTiO₂ with 5% SiO₂

1% cerium oxide=as reference, but TiO₂/SiO₂ replaced by cerium oxide upto a cerium oxide content of the catalyst of 1%

5% cerium oxide=as reference, but TiO₂/SiO₂ replaced by cerium oxide upto a cerium oxide content of the catalyst of 5%

10% cerium oxide=as reference, but TiO₂/SiO₂ replaced by cerium oxide upto a cerium oxide content of the catalyst of 10%

The catalysts were coated in the usual way on commercially availableflow-through substrates with a wash coat loading of 160 g/l and the NOxconversion was measured at GHSV=60000 1/h with the following test gascomposition:NOx: 1000 ppm

NO₂/NOx: 0% (FIG. 1) or 75% (FIG. 2) NH₃: 1100 ppm (FIG. 1) or 1350 ppm(FIG. 2) O₂: 10% H₂O:  5% N₂: Remainder

As shown in FIG. 1, the conversion of NO deteriorates as the content ofcerium oxide increases, while in FIG. 2, the conversion at NO₂/NOx=75%improves as the content of cerium oxide increases.

Example 1: Preparation of the Coating Suspensions (Wash Coats)

Preparation of Coating Suspension A (Vanadium SCR)

A commercially available titanium dioxide in the anatase form doped with5 wt % silicon dioxide was dispersed in water. Next, an aqueous solutionof ammonium metatungstate and ammonium metavanadate dissolved in oxalicacid were added as a tungsten or vanadium precursor in an amount suchthat a catalyst of composition 87.4 wt % TiO₂, 4.6 wt % SiO₂, 5.0 wt %WO₃ and 3.0 wt % V₂O₅ was the result. The mixture was stirred thoroughlyand finally homogenized in a commercially available agitator ball milland ground to d90<2 μm.

Preparation of Coating Suspension B (Vanadium SCR with 1% Cerium Oxide)

A commercially available titanium dioxide in the anatase form doped with5 wt % silicon dioxide was dispersed in water. Next, an aqueous solutionof ammonium metatungstate as a tungsten precursor, ammonium metavanadatedissolved in oxalic acid as a vanadium precursor, and an aqueoussolution of cerium acetate as a cerium precursor were added in an amountsuch that a catalyst of a composition that is calculated as 86.4 wt %TiO₂, 4.6 wt % SiO₂, 5.0 wt % WO3, and 3.0 wt % V₂O₅ and 1% CeO₂ was theresult. The mixture was stirred thoroughly and finally homogenized in acommercially available agitator ball mill and ground to d90<2 μm.

Preparation of Coating Suspension C (Fe SCR, SAR=25)

A coating suspension was prepared for a commercially available SCRcatalyst based on an iron-exchanged beta zeolite. For this purpose, acommercial SiO₂ binder, a commercial boehmite binder (as coating aids),iron(III) nitrate nonahydrate, and commercially available beta zeolitehaving a molar SiO₂/Al₂O₃ ratio (SAR) of 25 were suspended in water sothat a catalyst of composition 90 wt % β-zeolite and an iron content,calculated as Fe₂O₃, of 4.5 wt % was the result.

Preparation of Coating Suspension D (Fe-SCR, SAR=10)

A coating suspension was prepared for a commercially available SCRcatalyst based on an iron-exchanged beta zeolite. For this purpose, acommercial SiO₂ binder, a commercial boehmite binder (as coating aids),iron(III) nitrate nonahydrate, and commercially available beta zeolitehaving a molar SiO₂/Al₂O₃ ratio (SAR) of 10 were suspended in water sothat a catalyst of composition 90 wt % β-zeolite and an iron content,calculated as Fe₂O₃, of 4.5 wt % was the result.

Example 2: Preparation of the Catalyst Devices

Various catalyst devices were prepared by coating ceramic substrateswith coating suspensions A to D. Conventional ceramic monoliths withparallel flow channels (flow-through substrates) open at both ends wereused as substrates. In this case, a first and a second layer (S1, S2)were applied to each substrate, wherein each layer was subdivided intotwo adjacent zones (Z1, Z2). The exhaust gases to be purified flow inthe flow direction into the catalyst device, i.e. via the upper layer 2and from zone 1 to zone 2. In Scheme 1, the structure of the catalystdevices is shown with four catalytic regions located in two layers andtwo zones.

Scheme 1: Schematic structure of the catalyst devices produced accordingto the exemplary embodiments

Flow Direction→

Substrate Layer 2 Zone 1 Layer 2 Zone 2 (S2Z1) (S2Z2) Layer 1 Zone 1Layer 1 Zone 2 (S1Z1) (S1Z2)

The compositions and the amounts of coating suspensions A to D used aresummarized in Table 1 below. The table also shows which catalytic layersS1 and S2 and zones Z1 and Z2 were applied. The catalysts VK1 and VK3are comparative catalysts.

First of all, starting from the inlet side, one of dispersions A to Dwas applied by a conventional dipping method over the length of regionZ1S1 of a commercially available flow-through substrate having 62 cellsper square centimeter, a cell wall thickness of 0.17 millimeters and alength of 76.2 mm. The partially coated component was first dried at120° C., Next, starting from the outlet side, one of dispersions A to Dwas applied over the length of region Z2S1 by the same method. Thecoated component was then dried at 120° C., for 15 minutes at 350° C.,then calcined at 600° C. for a period of 3 hours. When dispersion andwash coat loading were identical in regions Z1S1 and Z2S1, one ofdispersions A-D was applied by a conventional dipping method to acommercially available flow-through substrate having 62 cells per squarecentimeter and a cell wall thickness of 0.17 millimeters over its entirelength of 76.2 mm. It was then dried at 120° C., for 15 minutes at 350°C., then calcined at 600° C. for a period of 3 hours.

Starting from the inlet side, the component thus calcined was thencoated according to the aforementioned method over the length of regionZ1S2 with one of suspensions A-D and dried at 120° C. Theabove-described step was skipped when no coating was provided for regionZ1S2. Starting from the outlet side, the coating was then applied overthe length of region Z2S2 using one of suspensions A-D. It was thendried at 120° C. The above-described step was skipped when no coatingwas provided for region Z2S2. It was then dried for 15 minutes at 350°C., then calcined at 600° C. for a period of 3 hours. When dispersionand wash coat loading were identical in regions Z1S2 and Z2S2, one ofdispersions A-D was applied over the entire length of the component of76.2 mm by the method described above. It was then dried at 120° C., for15 minutes at 350° C., then calcined at 600° C. for a period of 3 hours.

TABLE 1 Preparation of the catalyst devices having coating suspensions Ato D in the first and second (S1, S2) and in the first and second zone(Z1, Z2). This shows in each case the total quantity in g/l in each ofthe four regions (S1Z1 to S2Z2) after drying, calcination and heattreatment, and also the length of the zones in % based on the totallength of the catalyst device. The catalysts VK1 to VK4 are comparativecatalyts. Metal Coating suspension Z1S2 Z2S2 Z1S2 Z2S2 No. Z1S1 Z2S1Z1S1 Z2S1 VK1 Fe Fe 100 g/l C, L = 50% 100 g/l C, L = 50% V V 280 g/l A,L = 50% 280 g/l A, L = 50% VK3 Fe V 65 g/l D, L = 33% 140 g/l A, L = 67%Fe V 65 g/l D, L = 33% 140 g/l A, L = 67% K1 V V 280 g/l A, L = 50% 280g/l A, L = 50% Fe Fe 100 g/l C, L = 50% 100 g/l C, L = 50% K2 V—Ce V—Ce280 g/l B, L = 50% 280 g/l B, L = 50% Fe Fe 50 g/l C, L = 50% 50 g/l C,L = 50% K3 V V 160 g/l A, L = 50% 160 g/l A, L = 50% Fe Fe 100 g/l C, L= 50% 100 g/l C, L = 50% K4 V V 160 g/l A, L = 50% 160 g/l A, L = 50% FeFe 50 g/l C, L = 50% 50 g/l C, L = 50% K5 V V 280 g/l A, L = 50% 280 g/lA, L = 50% Fe Fe 50 g/l C, L = 50% 50 g/l C, L = 50% K6 V V 160 g/l A, L= 50% 160 g/l A, L = 50% Fe Fe 100 g/l D, L = 50% 100 g/l D, L = 50%

As an alternative to the described method, it would also be possible toprepare two catalysts (Z1, Z2) corresponding to zones Z1 and Z2described above and to test the two catalysts one after the other (Z1before Z2).

Catalyst Z1: First of all, apply one of dispersions A to D over theentire length of the substrate with the length Z1 (Z1S1 region), dry at120° C., then for 15 minutes at 350° C., then calcine at 600° C. for aperiod of 3 hours. If so intended, apply one of dispersions A to D overthe entire length of the component thus obtained (Z1S2 region), then[dry] for 15 minutes at 350° C., then calcine at 600° C. for a period of3 hours.

Catalyst Z2; First of all, apply one of dispersions A to D over theentire length of the substrate with the length Z2 (Z2S1 region), dry at120° 0, then for 15 minutes at 350° C., then calcine at 600° C. for aperiod of 3 hours. If so intended, next apply one of dispersions A to Dover the entire length of the component thus obtained (Z2S2 region),then [dry] for 15 minutes at 350° C., then calcine at 600° C. for aperiod of 3 hours.

Example 3: Reduction of Nitrogen Oxides by SCR

Measurement Method

The catalyst devices prepared according to Example 2 were tested fortheir activity and selectivity in the selective catalytic reduction ofnitrogen oxides. In doing so, the nitrogen oxide conversion was measuredat various defined temperatures (measured on the inlet side of thecatalyst) as a measure of the SCR activity and the formation of nitrousoxide. On the inlet side, model exhaust gases containing presetproportions of NO, NH₃, NO₂ and O₂, among other things, were introduced.The nitrogen oxide conversions were measured in a reactor made of quartzglass. Drill cores with L=3″ and D=1″ were tested between 190 and 550°C. under steady-state conditions. The measurements were taken under thetest conditions summarized below. GHSV is the gas hourly space velocity(gas flow rate:catalyst volume). The conditions of measurement seriesTP1 and TP2 are summarized below:

Test Parameter Set TP1:

Gas hourly space velocity GHSV=60000 1/h with the synthesis gascomposition: 1000 vppm NO, 1100 vppm NH₃, 0 vppm N₂O

a=xNH₃/xNO_(x)=1.1

xNO_(x)=xNO+xNO₂+XN₂O, wherein x in each case means a concentration(vppm) of 10 vol % O₂, 5 vol % H₂O, remainder N₂.

Test Parameter Set TP2

GHSV=60000 1/h with the synthesis gas composition:

250 vppm NO, 750 vppm NO₂, 1350 vppm NH₃, 0 vppm N₂O

a=xNH₃/xNO_(x)=1.35

xNO_(x)=xNO+xNO₂+xN₂O, wherein x in each case means a concentration(vppm) of 10 vol % O₂, 5 vol % H₂O, remainder N₂.

The nitrogen oxide concentrations (nitrogen monoxide, nitrogen dioxide,nitrous oxide) were measured downstream of the catalyst device. Thenitrogen oxide conversion over the catalyst device for each temperaturemeasurement point was calculated as follows from the nitrogen oxidecontents set in the model exhaust gas, which were verified duringconditioning at the beginning of particular test run with a pre-catalystexhaust gas analysis, and from the measured nitrogen oxide contentsafter the catalyst device (x is in each case the concentration in vppm):

U_(NOX)[%]=(1−X_(output)(NO_(x))/X_(input)(NO_(x)))*100[%]

with

X_(input)(NO_(x))═X_(input)(NO)+X_(input)(NO₂)

X_(output)(NO_(x))═X_(output)(NO)+X_(output)(NO₂)+2*X_(output)(N₂O).

X_(output)(N₂O) was weighted with the factor 2 in order to take thestoichiometry into account.

In order to determine the manner in which aging of the catalysts affectsthe result, the catalyst devices were subjected to hydrothermal agingfor 100 hours at 580° C. in a gas atmosphere (10% O₂, 10% H₂O, remainderN₂). Next, the conversions of nitrogen oxides were determined accordingto the method described above.

Results

The results of measurement series TP1, in which the model exhaust gascontained only NO as the nitrogen oxide, are summarized in Table 2. Theresults of measurement series TP2, wherein the model exhaust gascontained NO and NO₂ in the ratio 1:3 as the nitrogen oxides, aresummarized in Table 3. In each case, the tables indicate which catalystaccording to Example 2 (Table 1) was used. For each defined temperaturevalue, it is indicated what percentage of the initial concentration ofNOx was removed. Table 3 also specifies for each temperature value 2 to7 what absolute quantity of N₂O was measured at each temperature valueafter the catalyst. In FIGS. 1 to 5, the results are also showngraphically for the purposes of comparison. Tables 4 and 5 summarize theconditions and results of the tests with catalyst devices after aging.

FIGS. 1a, b show that catalysts K1 and K2 according to the invention, inwhich a first, upper layer with a vanadium catalyst overlies a second,lower layer with an iron exchanged zeolite, remove nitrogen oxidessignificantly more efficiently than a comparative catalyst VK1, in whicha layer with iron-exchanged zeolite overlies a vanadium oxide layer. Theeffect is particularly pronounced at temperatures below about 400° C.The effect is obtained even in the case of a model exhaust gas having ahigh NO₂ content of 66.7% (FIG. 1b ). FIG. 1c shows that significantlyless N₂O is formed with catalysts K1 and K2 according to the inventionthan with catalyst VK1. This effect is also particularly pronounced attemperatures below 400° C.

Catalysts K1 and K2 differ in that catalyst K2 contains a cerium oxidein the first, upper layer in addition to the vanadium oxide. The resultsshow that in particular in the temperature range below 350° C., afurther improvement is achieved by adding a cerium oxide, wherein boththe removal of NOx is further improved and the formation of N₂O isfurther reduced.

In FIG. 2, further comparisons of the conventional catalyst VK1 andcatalysts K1, K3, K4 and K5 according to the invention are shown ingraph form, wherein the catalysts according to the invention differ withregard to the amount of the catalysts used in the upper and lowerlayers. The results show that even with considerable variation in theamounts of catalyst, a significant effect is achieved. Catalyst K1 showsthe most pronounced effect in preventing the formation of N₂O (FIG. 2c).

FIG. 3 shows a comparison of the conventional catalyst VK1 and catalystsK3 and K6 according to the invention. FIG. 3 also demonstrates that thecatalysts according to the invention remove NOx considerably moreefficiently while significantly reducing the formation of N₂O.

FIG. 4 shows results for catalyst devices subjected to an artificialaging process as described above. FIG. 4 shows a comparison of theconventional catalyst VK1 with catalysts K1 and K2 according to theinvention. The results show that, even after aging, the catalystaccording to the invention depletes NOx significantly more efficientlyand reduces the formation of N₂O more than the comparative catalyst. Thetests also show that the advantages of having cerium oxide in thevanadium catalyst are particularly pronounced especially after aging.When adding cerium oxide, a more significant improvement of catalyst K2compared to the comparative catalyst but also compared to catalyst K1 isfound both in the depletion of NOx and in the prevention of nitrousoxide.

FIG. 5 shows further results obtained with catalysts after the agingprocess for catalysts K1, K4 and K5 according to the invention and forcomparative catalyst VK1. FIG. 5 also shows a marked improvement of thecatalysts according to the invention after aging with regard to the NOxdepletion and the prevention of the formation of nitrous oxide.

In the case of comparative catalyst VK3, the two catalysts are not inlayers one on top of the other, but the exhaust gases first enter a zonewith the iron-containing zeolite on the inlet side and then pass into anoutlet-side zone with the vanadium catalyst. The results summarized inTables 2 and 3 show that such a comparative catalyst not only exhibitscomparatively low conversions of NOx with both with exhaust gases richin NO and with exhaust gases rich in NO₂ but also causes a greaterformation of nitrous oxide.

Overall, the experiments show that the SCR catalysts according to theinvention, in which a vanadium oxide layer is disposed on a zeolitelayer containing iron, deliver significant improvements in the removalof NOx and the prevention of the formation of nitrous oxide. Thecatalyst devices according to the invention are suitable not only forthe reaction with exhaust gases rich in NO but also for the treatment ofexhaust gases rich in NO₂. The advantages with exhaust gases rich in NO₂are particularly pronounced in the temperature range below 450° C. orbelow 350° C. The catalyst devices according to the invention thuscombine several advantageous properties, namely a high efficiency withexhaust gases rich in NO₂ in the temperature range from about 180° C. to500° C., and in particular at low temperatures; a high efficiency withexhaust gases rich in NO; and the prevention of the formation of nitrousoxide. The effects are evident both with freshly prepared catalysts andafter an aging process. The effect can even be improved, if a ceriumoxide is added to the vanadium catalyst, which is in particularadvantageous in the case of aged catalysts.

TABLE 2 Conditions and results of the reduction of NO with differentcatalyst devices (test TP1) at different actually measured temperatures1 to 8. The depletion of NOx at the catalyst device outlet is shown in %based on the initial amount used. Test Temperature [° C.] NOx [%] TP 1 23 4 5 6 7 8 1 2 3 4 5 6 7 8 VK1 1 541 492 444 395 345 296 247 197 93%97% 96%  95%  91% 81% 56% 20% VK3 1 535 489 442 394 344 295 246 197 88%95% 98%  98%  97% 93% 73% 31% K1 1 543 496 449 400 350 300 251 201 67%93% 99% 100% 100% 98% 86% 44% K2 1 537 490 443 395 346 296 247 198 78%94% 98%  99%  98% 94% 76% 34% K3 1 542 496 448 400 350 300 251 201 76%96% 99% 100% 100% 97% 76% 31% K4 1 543 496 448 400 350 300 250 201 72%95% 99% 100% 100% 96% 72% 27% K5 1 543 496 448 400 350 300 251 201 65%92% 99% 100% 100% 98% 86% 42% K6 1 543 496 448 400 350 300 250 201 78%97% 100%  100% 100% 97% 80% 40%

TABLE 3 Test conditions and results of the reduction of NO₂:NO in theratio 3:1 (test TP2) at different actually measured temperatures. Formeasurements 2 to 7, the depletion of NOx at the catalyst device outletis shown in % based on the initial amount used and the measured valuesfor N₂O at the catalyst device outlet are shown in ppm. Test Temperature[° C.] NOx [%] Amount of N₂O [ppm] No. TP 2 3 4 5 6 7 2 3 4 5 6 7 2 3 45 6 7 VK1 2 492 445 397 347 298 249 98% 92% 81% 73% 66% 58% 10 40 92 127148 133 VK3 2 489 441 392 343 293 244 97% 95% 89% 80% 65% 62% 12 27 5683 98 56 K1 2 496 447 399 349 300 250 97% 99% 98% 86% 69% 60% 10 5 9 3983 92 K2 2 490 442 394 344 295 246 96% 97% 95% 90% 78% 82% 14 17 26 3869 76 K3 2 496 447 399 349 300 250 99% 99% 96% 84% 71% 62% 6 5 19 66 110113 K4 2 496 448 399 349 300 250 98% 98% 95% 82% 67% 60% 9 8 24 73 11083 K5 2 496 447 399 349 300 250 97% 99% 97% 83% 65% 58% 14 7 13 50 96 78K6 2 496 447 399 349 300 250 99% 99% 97% 86% 70% 59% 5 5 15 58 110 123

TABLE 4 Conditions and results of the reduction of NO with differentcatalyst devices after aging (test TP1) at different actually measuredtemperatures 1 to 8. The depletion of NOx at the catalyst device outletis shown in % based on the initial amount used. Test Temperature [° C.]NOx [%] No. TP 1 2 3 4 5 6 7 8 1 2 3 4 5 6 7 8 VK1 1 539 493 445 397 348298 249 200 79% 88% 91%  91% 87% 77% 53% 20% K1 1 542 496 448 400 350300 251 201 74% 95% 99% 100% 100%  97% 77% 31% K2 1 543 495 447 398 348299 249 199 70% 93% 97%  98% 97% 93% 71% 28% K4 1 542 496 448 400 350300 250 201 77% 95% 99% 100% 99% 90% 54% 17% K5 1 542 496 448 400 350300 250 201 68% 93% 99% 100% 100%  97% 77% 31%

TABLE 5 Test conditions and results of the reduction of NO₂:NO in theratio 3:1 (test TP2) with different catalyst devices after aging atdifferent actually measured temperatures. For measurements 2 to 7, thedepletion of NOx at the catalyst device outlet is shown in % based onthe initial amount used and the measured values for N2O at the catalystdevice outlet are shown in ppm. Test Temperature [° C.] NOx [%] Amountof N₂O [ppm] No. TP 2 3 4 5 6 7 2 3 4 5 6 7 2 3 4 5 6 7 VK1 2 494 446398 348 298 249 90% 87% 82% 74% 60% 57% 45 62 81 106 141 122 K1 2 495447 398 349 299 250 97% 99% 97% 80% 62% 56% 12 7 14 56 102 108 K2 2 495447 398 348 298 249 92% 95% 95% 92% 77% 60% 28 20 19 28 60 74 K4 2 495447 399 349 300 250 93% 94% 94% 76% 59% 56% 35 30 30 68 100 89 K5 2 495447 398 349 300 250 92% 96% 97% 81% 61% 56% 34 20 16 42 83 76

1. Catalyst device for purifying exhaust gases containing nitrogen oxideby selective catalytic reduction (SCR), comprising at least twocatalytic layers, the first layer containing vanadium oxide and a mixedoxide comprising titanium oxide and silicon oxide and the second layercontaining a molecular sieve containing iron, wherein the first layer isapplied onto the second layer.
 2. Catalyst device according to claim 1,wherein the first layer contains at least one further component selectedfrom oxides of tungsten and aluminum.
 3. Catalyst device according toclaim 1, wherein the first layer additionally contains cerium oxide. 4.Catalyst device according to claim 1, wherein the first layer comprisesthe following components: (a) from 0.5 to 10 wt % vanadium oxide,calculated as V₂O₅. (b) from 0 to 17 wt % tungsten oxide, calculated asWO₃, (c) from 0 to 10 wt % cerium oxide, calculated as CeO₂, (d) from 25to 98 wt % titanium oxide, calculated as TiO₂, (e) from 0.5 to 15 wt %silicon oxide, calculated as SiO₂, (f) from 0 to 15 wt % aluminum oxide,calculated as Al₂O₃, in each case based on the weight of the firstlayer.
 5. Catalyst device according to claim 1, wherein the molecularsieve is a zeolite.
 6. Catalyst device according to claim 5, wherein thezeolite is an iron-exchanged zeolite.
 7. Catalyst device according toclaim 5, wherein the zeolite has a structure, whose maximum ring sizehas more than 8 tetrahedra.
 8. Catalyst device according to claim 5,wherein the zeolite has a structure selected from AEL, AFI, AFO, AFR,ATO, BEA, GME, HEU, MFI, MWW, EUO, FAU, FER, LTL, MAZ, MOR, MEL, MTW,OFF and TON.
 9. Catalyst device according to claim 1, wherein the firstlayer is completely applied onto the second layer.
 10. Catalyst deviceaccording to claim 1, wherein the first layer is applied onto the secondlayer in certain regions.
 11. Catalyst device according to claim 1,wherein the second layer is applied onto an inert substrate, which ispreferably a ceramic monolith.
 12. A method of selective catalyticreduction (SCR), comprising utilizing a catalyst device according toclaim 1 for purifying exhaust gases containing nitrogen oxide byselective catalytic reduction (SCR).
 13. The method according to claim12 wherein the method, includes avoiding the formation of nitrous oxide.14. The method according to claim 12, wherein the exhaust gases have anNO₂/NOx ratio>0.5 and/or a temperature of 180° C. to 450° C.
 15. Methodfor purifying exhaust gases, comprising the steps of: (i) Providing acatalyst device according to claim 1, (ii) Introducing exhaust gasescontaining nitrogen oxides into the catalyst device, (iii) Introducing areductant containing nitrogen into the catalyst device, and (iv)Reducing nitrogen oxides in the catalyst device by selective catalyticreduction (SCR).